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| United States Patent |
5,112,587
|
|
von Wedel
, et al.
|
May 12, 1992
|
Method for the denitration of waste gases with obtention of HNO.sub.3
Abstract
A method for the removal of nitrogen oxides from waste gases and for
obtaining nitric acid is described. The waste gas is charged with the
required amount of hydrogen peroxide, converted into the gas phase, and
the gas mixture is reacted on a solid catalyst to hydrogen nitrate, which
is either withdrawn for further use or is converted into nitric acid
either by condensation or by scrubbing with water. The method permits the
removal of NO.sub.x at low concentrations below 2000 ppm with efficiencies
above 90%.
| Inventors:
|
von Wedel; Wedigo (Offenbach, DE);
Senff; Elke (Langenselbold, DE);
Helmling; Oswald (Hasselroth, DE)
|
| Assignee:
|
Degussa AG (Frankfurt am Main, DE)
|
| Appl. No.:
|
696011 |
| Filed:
|
May 6, 1991 |
Foreign Application Priority Data
| Current U.S. Class: |
423/235; 423/239.1; 423/393 |
| Intern'l Class: |
C01B 021/00; C01B 021/38; C01B 021/40; B01J 008/00 |
| Field of Search: |
423/390,393,235,239,239 A,235 D
|
References Cited
U.S. Patent Documents
| 4341747 | Jul., 1982 | Downey | 423/393.
|
| 4367204 | Jan., 1983 | Klopp et al. | 423/393.
|
| Foreign Patent Documents |
| 2537061 | Mar., 1976 | DE.
| |
| 2813370 | Oct., 1978 | DE | 423/390.
|
| 673409 | Mar., 1990 | CH.
| |
Primary Examiner: Heller; Gregory A.
Attorney, Agent or Firm: Beveridge, DeGrandi & Weilacher
Claims
We claim:
1. A method for the removal of nitrogen oxides from waste gases,
comprising: determining the content of nitrogen oxides of the waste gas,
treating the waste gas with a solution of hydrogen peroxide converted into
the gaseous state in an amount which is adapted to the amount of nitrogen
oxides in said waste gas to be removed and is at least stoichiometrically
sufficient for the reaction equations:
2 NO+3 H.sub.2 O.sub.2 .fwdarw.2 HNO.sub.3 +2 H.sub.2 O
and
2 NO.sub.2 +H.sub.2 O.sub.2 .fwdarw.2 HNO.sub.3,
to thereby obtain a gaseous reaction mixture containing the nitrogen oxides
and the hydrogen peroxide, reacting the gaseous mixture on a solid
catalyst which can absorb at least H.sub.2 O.sub.2 but which does not
excessively decompose the hydrogen peroxide, and thereafter withdrawing
the reacted gaseous mixture.
2. The method according to claim 1 wherein waste gases are treated that are
obtained from industrial furnaces or from combustion systems.
3. The method according to claim 1 wherein an excess of H.sub.2 O.sub.2 is
used.
4. The method according to claim 1 wherein the gaseous reaction mixture is
reacted at its temperature or with an adjustment of the gaseous mixture
temperature into the range of 20.degree. to 120.degree. C.
5. The method according to claim 1 wherein the solid catalyst is used in an
amount to insure a space velocity up to 260 m.sup.3 /h/kg.
6. The method according to claim 1 wherein the amount of gaseous NHO.sub.3
/H.sub.2 O mixture formed is processed further to form nitric acid.
7. The method according to claim 1, further comprising carrying out the
reaction in a fluidized bed or fixed bed of the catalyst.
8. The method according to claim 1 wherein said catalyst is a member of the
group:
a) as fine or granulated substances:
silica gels, precipitated silicas, pyrogenic silicas, optionally in
hydrophobic form;
wide-pore or medium-pore natural or synthetic zeolites;
ion-exchange resins with porous structure;
phyllosilicates;
diatomaceous earth;
aluminum oxide;
titanium dioxide;
natural or synthetic laminated silicates;
activated carbons;
b) microglass spheres
quartz sand;
calcium sulfate hydrate powder, optionally as granulate
narrow-pore zeolites, optionally as a granulate;
c) builder's sand; and
iron oxide,
and mixtures thereof.
9. The method according to claim 1 further comprising bringing aqueous
hydrogen peroxide in a concentration up to 85% by weight in the required
measured amount for evaporation into a stream of waste gas.
10. The method according to claim 9 wherein the aqueous hydrogen peroxide
is sprayed or atomized into the stream of waste gas.
11. The method according to claim 9 wherein the aqueous hydrogen peroxide
is evaporated by means of an external evaporator of an evaporator arranged
in the stream of waste gas.
12. The method according to claim 11 wherein a falling-film evaporator is
used, with adjustment of the evaporation amounts via the amount of H.sub.2
O.sub.2 solution supplied to the evaporator.
13. The method according to claim 1 further comprising reacting the gas
mixture on the catalyst a plurality of times.
14. The method according to claim 13 wherein an additional amount of
H.sub.2 O.sub.2 is used.
15. The method according to claim 13 wherein the HNO.sub.3 contained in the
gaseous reaction mixture is sorptively removed.
16. The method according to claim 1 further comprising scrubbing said
gaseous HNO.sub.3 /H.sub.2 O mixture formed by means of scrubbing with
water or optionally dilute nitric acid with a concentration above 10% by
weight in the gas phase and the residual gas which was not absorbed in the
scrubbing process is removed.
17. The method according to claim 16, further comprising recycling the
scrubbing liquid for enriching the nitric acid and removing concentrated
nitric acid.
18. The method according to claim 16 further comprising treating withdrawn
residual gas before discharging into the atmosphere in a scrubbing stage
with water or dilute nitric acid with a concentration up to 10% by weight.
Description
BACKGROUND OF INVENTION
The present invention relates to a method for the removal of nitrogen
oxides, especially of NO and/or NO.sub.2 from waste gases of many kinds,
especially waste gases obtained from industrial furnaces and from
combustion firing systems. The present invention further relates to a
method for the recovery of nitric acid.
For reasons of environmental protection, effective methods for an extensive
removal of nitrogen oxides from industrial systems, e.g. the production of
fertilizers or the processing of metals, but also from combustion furnaces
systems of varied types, including power plants and garbage incineration
plants, are becoming more and more important. The value of these methods
is to be judged on the basis of the extent to which the pollutants can be
removed and whether harmless conversion products are created in those
methods or whether utilizable by-products, that is, valuable substances,
are formed.
Methods have already been described by which waste gases of varied origins
containing nitrogen oxide were subjected to a gas scrubbing operation for
the physical or chemical absorption of the nitrogen oxides. Since
primarily nitrogen dioxide, NO.sub.2, and nitrogen monoxide, NO, are
contained in such waste gases and since the latter is especially difficult
to absorb in aqueous media, the suggestion has been made in DE-AS 25 37
061 that the NO be catalytically oxidized before the gas scrubbing.
The nitrogen dioxide formed can be removed from the waste gas basically by
means of absorption in water. However, a sufficient reduction of its
concentration can not be achieved in a satisfactory manner in the case of
low concentration waste gases (e.g. <2000 ppm NO.sub.2) when using the
conventional apparatus in practice in large-scale purification of waste
gases. This is due to the economically imposed conditions limiting the
dwell times (e.g. to values below approximately 2 sec.) as a consequence
of the rate of dissolution, which is still too low.
Even a reaction of dissolved nitrogen dioxide by means of a chemical
reaction with oxidation agents, alkali metal hydroxide or ammonia, which
are added to the absorption agent with the intention of achieving an
acceleration of the absorption by means of a spontaneous removal of
dissolved nitrogen dioxide from the solution equilibrium, has not resulted
in the desired success. In spite of the addition of NaClO.sub.2 as an
oxidation agent, rates of absorption which were barely greater than 50%
were able to be achieved under industrial conditions, that is, in the case
of NO.sub.x amounts of Y.sub.NOx .ltoreq.1000 ppm, dwell times in a
waste-gas scrubber of <1 sec. and temperatures >40.degree. C. An
aggravating circumstance is the fact that, at least in the case of
combustion waste gases, alkaline scrubbing solutions can not be
economically used because of the alkali consumption by CO.sub.2. Even the
addition of solubilizers (metal-chelate complexes) was not able to improve
oxidative gas scrubbing to any considerable degree.
The currently dominant method for the denitration of waste gases relies on
the reduction of nitrogen oxides to nitrogen and water. This can take
place either catalytically (SCR) or non catalytically by means of the use
of high temperatures (SNCR). Ammonia is usually used as the reduction
agent in both methods. However, SCR and SNCR systems for the denitration
of waste gases have the disadvantage of a greater or lesser ammonia
leakage.
There are other disadvantages in addition to the ammonia leakage. There is
the necessity of keeping in reserve rather large amounts of liquid
ammonia, which is associated with a potential danger for the surrounding
population. The SCR method requires relatively expensive catalysts. Since
both methods are carried out at an elevated temperature, the accumulating
waste gases, which are cooler, must be preheated. The harmless compounds
nitrogen and water are produced as reaction products; they do not
constitute useful substances which can be used further.
An attempt has also been made to treat nitrogen-oxide-containing waste
gases with aqueous solutions of hydrogen peroxide in a scrubbing method.
This method has also not resulted in the past in any palpable success
since the degrees of denitration achievable in the case of waste gases
containing a low concentration of nitrogen oxides and requiring rather
long scrubbing times were not even approximately sufficient.
An object of the invention is to provide a method for the purification of
nitrogen-oxide containing waste gases, especially those with low
concentrations of NO.sub.x, that is, concentrations <1000 ppm NO.sub.x,
which permits degrees of denitration above 90% even at low temperatures
and drastically reduced dwell times and in which the nitrogen oxides can
be converted practically completely into a useful substance, namely, to
nitric acid.
SUMMARY OF THE INVENTION
In attaining the above as well as other objects, one feature of the
invention resides in a method for the removal of nitrogen oxides,
especially of NO and/or NO.sub.2 from waste gases, especially from waste
gases from industrial furnaces and from combustion systems, with the
recovery of nitric acid. A feature of the method of the invention resides
in first determining the content of nitrogen oxides of the waste gas and
then charging the waste gas with a solution of hydrogen peroxide converted
into the gaseous state in an amount which is adapted to the amount of
nitrogen oxides to be removed.
Another feature of the invention is to determine the amount of hydrogen
peroxide to be stoichiometrically sufficient for the reaction equations:.
2 NO+3 H.sub.2 O.sub.2 .fwdarw.2 HNO.sub.3 +2 H.sub.2 O
and
2 NO.sub.2 +H.sub.2 O.sub.2 .fwdarw.2 HNO.sub.3
In an optional embodiment, the hydrogen peroxide is present in excess.
In carrying out the invention, the gaseous mixture is reacted either at its
temperature or preferably with adjustment of the temperature of
20.degree.-120.degree. C. on a solid substance as catalyst. The catalyst
can adsorb at least H.sub.2 O.sub.2 because of its increased outer surface
area and/or because of an existing inner surface area. However, the
catalyst does not decompose the hydrogen peroxide, or does not decompose
it excessively. The reacted gaseous mixture so obtained is then withdrawn
for further processing. Alternatively, the amount of gaseous HNO.sub.3
/H.sub.2 O mixture formed in the reaction and present in the gaseous
mixture is processed further to form nitric acid in accordance with known
procedures such as condensation or scrubbing with water. The nitric acid
is then recovered as an economically useful product of the waste gas
purification system.
The test results show that that a part of the NO present in the gas current
is converted by a side reaction into NO.sub.2 according to the reaction:
NO+H.sub.2 O.sub.2 .fwdarw.NO.sub.2 +H.sub.2 O.
Consequently, not only is HNO.sub.3 formed but also, to the extent that NO
is present, NO.sub.2 can result as a reaction product from this reaction.
However, if a sufficient supply of H.sub.2 O.sub.2 is kept in reserve,
NO.sub.2 is oxidized further to HNO.sub.3.
The reaction can be carried out in a fluidized bed or in a fixed bed of the
solid catalyst; however, a fluidized bed is preferred.
The use of the solid catalyst in a fluidized bed permits a smaller particle
size and an improved conversion of substance and heat between the gaseous
phase and the catalyst. A smaller particle size for the catalyst is
advantageous in the given, rapid chemical reaction since a better
utilization of the catalyst is obtainable because of shorter diffusion
paths and because of the enlarged outer surface area. In addition, the
reaction heat is more efficiently removed in a fluidized bed than in a
fixed bed.
The use of a fixed-bed reactor is recommended when using a less
abrasion-resistant catalyst and in instances in which only a partial
denitration with low pressure loss is necessary.
Experimentally, a degree of denitration of above 70% at temperatures
between 40.degree. C. and 100.degree. C. was able to be realized in the
past (at 750 ppm NO.sub.x) in a fixed-bed reactor at a space velocity of
66.7 m.sup.3 /h/kg.
The selection of the solid catalyst is not critical because any finely
divided and/or porous and/or rough-walled solid substances can be used for
purposes of the invention to the extent that the catalyst does not
decompose hydrogen peroxide, or does not excessively decompose it and, of
course, is chemically resistant to the reactants and reaction products.
The proven suitability of a plurality of substances that are conventionally
used for catalytic carriers or adsorbents shows that the catalyst in the
process of the invention acts practically only by means of its surface
area characteristics, which is elevated in relation to the walls of
customary reaction containers.
The substance groups designated in the following list with a), b) and c),
wherein the effectiveness decreases from a) to c), were found to be
suitable as catalysts in an experiment carrying out the present invention.
Substances which proved to be totally unsuitable were so-called reflex
beads of glass (Belletini company) or ion-exchange resins totally free of
pores (e.g. Lewatit S 100, order No. 2-100, Bayer) or manganese(IV)-oxide
in powder form, which, as is known, decomposes hydrogen peroxide
particularly rapidly.
The substances which were tested and found to be suitable are all available
at low cost:
a) Silica gels, precipitated silicas, pyrogenic silicas, optionally in
hydrophobic form in each instance;
Wide-pore or medium-pore natural or synthetic zeolites;
Ion-exchange resins with porous structure;
Phyllosilicates;
Diatomaceous earth;
Aluminum oxide;
Titanium dioxide;
Natural or synthetic layered silicates; and
Activated carbons;
but also
b) Microglass spheres;
Quartz sand;
Calcium sulfate hydrate powder; and
narrow-pore zeolites
and even
c) Builder's sand; and
Iron oxide.
The catalysts which were tested in more detail in experiments are
characterized more specifically in the following:
Silica gel 60, particle size 0.2-0.5 mm, specific surface approximately
450-500 M.sup.2 /g (item 7733 of the Merck company, Darmstadt);
Silica gel 60 H, silanized (item 7761 of the Merck company, Darmstadt);
Wide-pore 12-ring zeolite, mordenite (pore width 6.7.times.7.0 .ANG.,
modulus 18 (Si/Al=9));
Wide-pore 12-ring zeolite, dealuminized y-zeolite (pore width 7.4 .ANG.,
modulus 200 (Si/Al=100));
Wide-pore 12-ring zeolite, NH.sub.4 -y zeolite (pore width 7.4 .ANG.,
modulus 5 (Si/Al 2.5)) as well as
Medium-pore 10- ring zeolite, ZSM-5 (pore width 5.4-5.6 .ANG., modulus 42
(Si/Al 21));
Ion-exchange resin, macroporous, sharply acidic (Amberlyst 15, item 15635
of the Merck company, Darmstadt); diatomaceous earth, annealed -
commercial product;
Aluminum oxide 90 (item 1078 of the Merck company, Darmstadt);
Titanium dioxide (item 812 of the Merck company, Darmstadt);
Calcium silicate hydrate, contained in CATSAN--hygienic (sanitary) litter
of the Effem company, Verden/Aller; and
Activated carbon with a specific surface of 1270 m.sup.2 /g and an average
pore diameter of 160 .mu.m (active carbon carrier 120, Degussa,
Frankfurt).
All these substances are excellent catalysts.
The following can be used with a medium action:
Glass spheres (window glass, particle size 1-40 .mu.m) (microglass spheres
type: 3000 of the Potters-Ballotini GmbH company, Kirchheimbolanden);
Quartz sand 0.4-0.6 mm particle size (screen size) (type P, Busch company,
Schnaittenbach);
Precipitated powdery calcium sulfate (item 2160, Merck company, Darmstadt);
and
Narrow-pore zeolite (Na-A, pore diameter 4 .ANG., modulus 2 (Si/Al=1)).
The following can be used with a weak action:
Builder's sand, particle size 0.05-0.6 mm; and
Iron(III)oxide powder.
BRIEF DESCRIPTION OF DRAWING
The drawing illustrates the flow chart of the method of carrying out the
present invention.
DETAILED DESCRIPTION OF INVENTION
The FIGURE represents a schematic flow diagram of the operation of the
experiment described herein in the examples. A source of NO gas in a
container (1) is conducted through a valve equipped pipe line (1A) to a
mixing device 2 which is also charged with a source of pressurized air
(1B). The composite gaseous mixture is then conveyed through flow meter
(4) to the falling film evaporator (6).
A source of H.sub.2 O.sub.2 is located in tank (7) located above the
falling film evaporator (6).
For analyzing the model gas, valve (3) is opened and the gas mixture flows
to a commercial NO.sub.x analyzer (5).
From falling film evaporator (6), the gas --H.sub.2 O.sub.2 stream flows
into fluidized bed reactor (9) and from there to filler column (10).
According to a preferred embodiment of the method of the invention, aqueous
hydrogen peroxide in a concentration up to 85% by weight in the required
measured amount for evaporation is brought into a stream of waste gas,
optionally by means of spraying or atomizing. Alternatively, the
evaporation is performed by means of an external evaporator or an
evaporator arranged in the stream of waste gas, preferably a falling-film
evaporator, with adjustment of the evaporation amounts by way of the
amount of H.sub.2 O.sub.2 solution supplied to the evaporator.
A single fluid or two-fluid nozzle can be used for spraying, through which
the hydrogen-peroxide solution is fed directly into the NO.sub.x
-containing gas stream to be treated and is converted there into the vapor
phase. An atomization takes place preferably with a suitable commercial
ultrasonic atomizer.
If the hydrogen peroxide solution is vaporized using a falling-film
evaporator, then either the gas vapor stream to be treated can flow
through the evaporator as the receiver phase for the hydrogen peroxide to
be evaporated or an auxiliary gas stream can flow through it as receiver
phase. The latter is then mixed, after being charged with hydrogen
peroxide solution, with the gaseous stream to be treated and supplied to
the catalytic component.
Hydrogen peroxide solution is supplied in a known flow amount in a
continuous manner by a dosing pump from a thin hose or tube onto the upper
part of the heated substance-exchange surface of the evaporator. It flows
downward by gravity, during which time a continuous and complete
vaporization takes place.
An especially simple embodiment for an externally situated falling-film
evaporator through which a stream of auxiliary gas flows consists of a
filler column onto the upper end of which the hydrogen peroxide solution
is located in a storage container and through which warm carrier air flows
from below with the aid of a hot-air blower. The evaporation can also be
carried out by dosing the hydrogen peroxide solution onto an evaporation
surface around which the gas to be treated flows and which is sufficiently
heated by its thermal content for a complete vaporization. This can be
realized, for example, by means of a packing of glass spheres in the gas
stream, onto which the H.sub.2 O.sub.2 solution is dripped or sprayed.
In order to increase the total effectiveness of the method of the invention
as regards the removal of nitrogen oxide, the gas mixture reacted on the
catalyst can be catalytically reacted again, optionally after another
charging with H.sub.2 O.sub.2, and further optionally after a sorptive
lowering or removal of the HNO.sub.3 contained in the gas mixture, for a
further reduction of nitrogen oxides which are still contained in gas
stream.
This step can be repeated once or several times, as required. A new
charging with H.sub.2 O.sub.2 after a first denitration stage can be
eliminated if the waste gas from this stage still contains a sufficient
amount of H.sub.2 O.sub.2 which has not yet been utilized. The sorptive
removal of the hydrogen nitrate HNO.sub.3 formed after a preceeding
catalytic reaction with H.sub.2 O.sub.2 can take place by means of an
absorption, e.g. in water or in dilute nitric acid.
A scrubbing column or tower is used for this step. However, it can also
take place by means of a physical adsorption, e.g. on activated carbon or
another suitable adsorption agent. Another possibility consists of a
chemical reaction with a reactive solid such as, for example, lime.
A continued reduction of the NO.sub.x concentration is achieved by means of
the single or multiple repeated catalytic treatment of the gas in the
presence of gaseous hydrogen peroxide. However, since degrees of
denitration of above 90% can be achieved even in the case of relatively
dilute NO.sub.x --containing gases (<1000 ppm NO.sub.x) even with a single
treatment of the described type, a multi-stage treatment is usually not
necessary. However, the situation is quite different in the case of gases
containing more concentrated amounts of NO.sub.x. In this instance, a
multi-stage treatment is often necessary, since as a result of the limited
ability of the gas phase to be loaded with H.sub.2 O.sub.2, which
limitation is caused by the dew point, only an equivalent amount of the
nitrogen oxides can be reacted to HNO.sub.3.
The gaseous phase must accordingly be recharged with H.sub.2 O.sub.2 and
brought into contact again with one of the suggested catalysts in order to
achieve the desired degree of denitration. If necessary, the HNO.sub.3
stemming from the preceding reaction is entirely or partially removed from
the gas phase before the recharging of the gas with H.sub.2 O.sub.2.
The reaction heat occurring during the reaction can also require a stepwise
performance of the reaction since problems can otherwise occur with the
container material. The stepwise carrying out of the reaction can take
place in fixed-bed reactors or in fluidized bed reactors containing one or
more of the, for example, preferable described catalysts. Optionally,
auxiliary agents can be used, for example, for improving the flowability
or for pelletizing.
If liquid nitric acid is to be obtained as a useful substance, the gaseous
HNO.sub.3 /H.sub.2 O mixture formed in the method is depleted by means of
scrubbing with water or preferably dilute nitric acid with a concentration
above 10% by weight in the gas phase. The residual gas which is not
absorbed in the scrubbing process is removed, optionally for further
treatment.
As high a concentration as possible of the primarily accumulating acid is
to be sought in the recovery of liquid nitric acid for reasons of better
marketing and for a more economical subsequent concentration and/or
purification. Therefore, the nitric acid can be recycled and functions as
a receiver phase for HNO.sub.3 present as gas and for H.sub.2 O.
The maximum obtainable concentration of nitric acid is the one which is
adjusted by means of the evaporation equilibrium liquid nitric acid/gas
phase. The water content and the HNO.sub.3 content of the ga downstream of
the reactor as well as the temperature at which the scrubbing stage is
operated are of great significance.
Since the values of these parameters can be very different from case to
case, no generally applicable statement can be made about the maximum
obtainable concentration of the nitric acid circulating in the scrubber.
However, the concentration can be calculated in the individual instance
according to customary methods, given knowledge of the relevant values in
the particular case.
In order to achieve a concentration of the nitric acid, the scrubbing
liquid can be recycled, at which time the concentrated nitric acid is
removed as needed.
In order to obtain a waste gas from the described method which is as clean
as possible, the residual gas that is withdrawn after the HNO.sub.3 was
scrubbed out can be treated in accordance with a preferred embodiment of
the method of the invention prior to being discharged into the atmosphere
in a scrubbing stage with water or dilute nitric acid in a concentration
up to 10% by weight.
The use of nitric acid of the highest possible concentration as the
receiver phase for a HNO.sub.3 /H.sub.2 O mixture which accumulates in a
gaseous form has the consequence that the gas taken off from the
absorption apparatus still contains HNO.sub.3 in a concentration which
results from the gas/liquid equilibrium.
It can be necessary to this end, in order to observe officially mandated
conditions, to connect a subsequent, second scrubbing stage downstream
which further reduces the emission of HNO.sub.3. This second scrubbing
stage is operated with water or nitric acid in a concentration up to 10%
by weight. In order to prevent a too great concentration of HNO.sub.3 from
arising in this stage, fresh water must be introduced as required and a
part of the circulation solution discharged. This discharged circulation
solution, slightly charged with HNO.sub.3, from the subsequently
connected-in wash is supplied to the bottom of the preceding wash as
scrubbing agent. This avoids the accumulation of nitrate-charged waste
water from the subsequently connected-in scrubbing step.
The effectiveness of the method can generally be checked as follows:
A stream of model gas loaded with nitrogen oxides through a falling-film
evaporator in which a continuously supplied, 50% by weight aqueous
solution of hydrogen peroxide is completely vaporized in a concurrent flow
with the stream of model gas. The maximum concentration of H.sub.2 O.sub.2
in the model-gas stream is limited by the dew point of the gaseous
hydrogen peroxide/water mixture at the temperature of the gas stream.
Thus, H.sub.2 O.sub.2 contents of up to approximately 2000 ppm H.sub.2
O.sub.2 (.congruent.2790 mg H.sub.2 O.sub.2 /m.sup.3) were achieved at a
temperature of 20.degree. C. and normal pressure. At higher temperatures,
the absorption capacity of the model gas for H.sub.2 O.sub.2 increases in
accordance with its vapor-pressure curve.
The gas leaves the falling-film evaporator, heated to 70.degree. C., and
passes into the reactor. The catalyst is located there, preferably in the
form of a fluidized bed consisting of a finely divided solid material
which is inert in the reaction medium, which aids the reaction by virtue
of a geometric and/or inner surface area or adsorption action which is
greater in surface area in comparison to the reactor wall and which does
not decompose H.sub.2 O.sub.2 or does not significantly decompose it.
Here, amounts of the catalyst were used which permit space velocities
between 18 and 260 m.sup.3 /h/kg.*)
*) For applications in industrial scale generally space velocities up to
260 m.sup.3 /h/kg and above may be used.
The nitrogen oxides are reacted catalytically with the hydrogen peroxide to
form HNO.sub.3 in the reactor, during which process this compound
accumulates in a gaseous form, is taken up by the stream of model gas
together with the water vapor stemming from the reaction of NO and is
discharged out of the reactor.
If the gas is not to be further used as such, for example, for the
production of fertilizers, it is then passed in the simplest instance
directly into a scrubbing system for the generation of nitric acid. The
HNO.sub.3 content is washed out in this system with the aid of water or
dilute nitric acid in a concentration above 10% by weight. This succeeds
very readily because gaseous HNO.sub.3 is readily soluble in aqueous
media. Any non-reacted remnants of nitrogen oxides dissolve only very
little in the scrubbing stage and therefore leave the system for an
optional further workup. The waste gas can also still contain amounts of
HNO.sub.3 in a concentration which can be approximately indicated via the
liquid/gas phase equilibrium of the scrubbing liquid.
The degrees of denitration achieved in a laboratory experiment are above
90% when using a silica gel as catalyst if the raw gas contains 720 ppm
NO.sub.x and a concentration of 1200 ppm H.sub.2 O.sub.2 is adjusted.
The method of a simple embodiment presented above in a general form can be
set up as a first stage in a practical method for carrying out the
invention. This stage would then include a) the addition and vaporization
of peroxide, b) reaction of the peroxide with the nitrogen oxides in the
catalytic fluid bed and c) an absorption of the gaseous HNO.sub.3 formed
in at least 10% by weight nitric acid. Very high degrees of denitration
can be achieved with several stages of a) plus b) and a subsequent wash
following c). Denitration can reach almost 100%.
The influence of the NO.sub.x amount contained in the gas to be treated is
as follows:
______________________________________
Conditions:
Model gas, fluidized bed reactor
Temperature: 25.degree. C.
Gas stream: 2.3 Nm.sup.3 /h
Catalyst: 30 g silica gel 60
H.sub.2 O.sub.2 50% solution:
0.08 ml/min.
______________________________________
Inlet, NO 1625 875 470 250 20
ppm NO.sub.x
2250 1250 690 400 90
NO.sub.2
625 375 220 150 70
Outlet, NO 650 200 20 0 0
ppm NO.sub.x
1500 875 70 35 25
NO.sub.2
850 675 50 35 25
Degree of 33.3 30.0 89.9 91.3
72.2
denitration %
______________________________________
The amount of NO.sub.x removed decreases with decreasing concentration of
NO.sub.x in the model gas. At the very low NO.sub.x content of 90 ppm, a
degree of denitration of 72.2% is still achieved; however, the H.sub.2
O.sub.2 supplied is no longer completely utilized. In the case of higher
concentrations of NO.sub.x (2250 ppm and 1250 ppm), there is a deficiency
of H.sub.2 O.sub.2. The denitration was improved here by adding more
H.sub.2 O.sub.2 ; however, the dew point sets an upper limit in this
instance.
The influence of the supply of H.sub.2 O.sub.2 is as follows:
__________________________________________________________________________
Conditions:
Model gas, fluidized bed reactor
250 ppm NO
400 ppm NO.sub.x
(150 ppm NO.sub.2)
Catalyst: 30 g silica gel 60
Temperature: 25.degree. C.
Gas stream: 2.3 Nm.sup.3 /h
__________________________________________________________________________
50% solution of
0.08
0.06
0.04
0.035
0.03
0.025
0.02
H.sub.2 O.sub.2 ml/min.
Clean gas
NO 0 2 6 9 .sup..about. 0
.sup..about. 0
.sup..about. 0
ppm NO.sub.x
35 35 35 38 160 260 350
NO.sub.2
35 33 29 29 160 260 350
Degree of 91.3
91.3
91.3
90.5
60.0
35.0
12.5
Denitration %
__________________________________________________________________________
It is clear from the data that an increase of the H.sub.2 O.sub.2 supply is
only logical if a certain lower limiting concentration of NO.sub.x,
influenced to a large extend by the structural conditions of the
apparatus, (in the current instance approximately 30 ppm NO.sub.x) had not
already been reached in the clean gas.
The influence of the temperature is as follows:
______________________________________
Conditions:
Model gas, moistened with water,
Fluidized bed reactor
470 ppm NO
720 ppm NO.sub.x
(250 ppm NO.sub.2)
Catalyst: 30 g silica gel 60
Gas stream: 2.3 Nm.sup.3 /h
H.sub.2 O.sub.2 50% solution:
0.08 ml/min.
______________________________________
Reactor 25 40 55 80 95 110 130
temperature, .degree.C.
NO, ppm 11 6 15 40 50 70 100
NO.sub.x, ppm
62 66 76 100 130 180 240
NO.sub.2, ppm
51 60 61 60 70 110 114
Degree of 91.4 90.8 89.4 86.1
81.9
75 66.7
Denitration %
______________________________________
As the temperature rises, the degree of denitration deteriorates, slightly
at first, then increasingly more sharply. This tendency could be
counteracted by means of a greater amount of catalyst.
The influence of the amount of catalyst in the fluid bed is as follows:
______________________________________
Conditions:
Model gas, fluidized bed
480 ppm NO
700 ppm NO.sub.x
(220 ppm NO.sub.2)
Catalyst: silica gel 60
Temperature: 40.degree. C.
Gas stream: 1.6 Nm.sup.3 /h
H.sub.2 O.sub.2 50% solution:
0.08 ml/min.
______________________________________
Amount of catalyst, g 15 30 60
Clean gas, NO 30 20 0
ppm NO.sub.x
110 70 30
NO.sub.2
80 50 30
Degree of Denitration, % 84.3 90.0 95.7
______________________________________
Increasing of the quantity of catalyst at a given volume of gas stream flow
to be treated (i.e. decreasing of the space velocity) brings about an
increased conversion of the nitrogen oxides to HNO.sub.3.
Further conceivable influencing variables on the conversion, such as the
moisture of the raw gas (potential competing adsorption of H.sub.2 O.sub.2
/NO/NO.sub.2 with H.sub.2 O) or the additional presence of SO.sub.2 as
well as both influencing variables together, have been investigated in
experiments.
After the humidifying of the model gas, a somewhat reduced denitration
effect occurred. However, high degrees of denitration continue to be
present (see examples).
In the case of a humidifed model gas containing SO.sub.2 in addition, no
lesser denitration effect occurred than in the case of dry model gas free
of SO.sub.2 (see examples). However, the SO.sub.2 was completely reacted
to SO.sub.3. As a consequence, SO.sub.3 aerosols formed above the catalyst
(silica gel 60). The color of the catalyst changed during operation after
the start of the addition of H.sub.2 O.sub.2 from white to orange, whereas
by way of contrast in the case of dry model gas free of SO.sub.2, a color
change from white to yellow took place.
The method of the present invention has the following advantages:
1. It can be used at temperatures below 100.degree. C. and can thus be
operated as a denitration stage connected downstream of a wet method for
desulfurization and for purifying cold process gases.
The method generates, with gaseous HNO.sub.3 or with liquid nitric acid, a
utilizable substance from the nitrogen oxides.
2. The dimensions of the HNO.sub.3 absorber can be kept relatively small
since, according to the invention, the nitrogen oxides are reacted
catalytically to the compound HNO.sub.3, which is readily soluble in
aqueous media, without being brought beforehand into a liquid phase.
3. As a consequence of the use of hydrogen peroxide, which is particularly
compatible with the environment, the method is free of additional
emissions of pollutants caused e.g. in the SCR or SNCR methods.
4. The method is distinguished by the use of especially economical
catalysts which are, in addition, not sensitive to so-called catalytic
poisons, since their effectiveness is assured by their large surface and
not by relatively few active centers.
5. The method is also suitable for very small emission sources because of
the low capital expenditure required and its simple design.
6. The method achieves degrees of denitration of above 90% with a one-stage
operation even in the case of small concentrations of NO.sub.x. If several
stages are used, an almost complete removal of NO.sub.x can be realized.
7. The desired degree of denitration can be readily adjusted by way of the
amount of hydrogen peroxide added.
8. The method operates completely without waste water and refuse. No
residual substances requiring disposal accumulate.
EXAMPLES
The invention is explained further in the following using examples of
embodiments with different catalysts. Example 1 contains a description of
the apparatus used in all examples.
Example 1
A model gas is produced by mixing compressed air and a slight amount of NO
gas taken from gas bottle 1 and is conducted through mixing stretch 2 into
falling film evaporator 6 (material: glass). The volume flow is 2.3
Nm.sup.3 /h. It is indicated by float flow meter 4. The model gas is
analyzed for its content of NO and NO.sub.x as required after the opening
of valve 3 with a commercially NO.sub.x analyzing device 5
(chemiluminescence principle). The difference of the concentration of
NO.sub.x and of NO yields the concentration of NO.sub.2. The NO.sub.2 is
formed by air oxidation from NO.
During its passage through the falling film evaporator, the model gas is
charged with a defined amount of vaporized solution of H.sub.2 O.sub.2.
Automatic dosing device 7 is used for this, with which a 50% aqueous
solution of hydrogen peroxide is continuously fed onto the evaporation
surface of the falling film evaporator around which the model gas flows.
The evaporation surface is heated with warm water controlled by a
thermostat to 80.degree. C. The dosed solution of H.sub.2 O.sub.2 runs in
at a dosing rate of 0.08 ml/min. onto the upper end of the evaporation
surface and flows down on it under the influence of gravity. During its
downward travel, the solution of H.sub.2 O.sub.2 evaporates completely, is
taken up by the model gas and carried along with it.
The gas current charged in this manner with solution of H.sub.2 O.sub.2
passes into fluid-bed reactor 9 (material: glass), which contains the
catalyst (60 g silica gel 60, particle size 0.2-0.5 mm, item 7733 of the
Merck company, Darmstadt).
The reactor is conically designed. The empty tube velocity of the gas is
0.33 m/s in the lower part with the smallest cross section. The reactor is
equipped with a thermometer.
Following reactor 9, the reacted gas mixture is conducted into a filler
column 10 (material: glass, diameter 4 cm, length, 40 cm, packing: Raschig
rings 2.times.4 mm, cocurrent operation). The HNO.sub.3 formed in the
reactor is absorbed here at room temperature with recycled water which is
gradually converted into dilute HNO.sub.3. The non-reacted nitrogen-oxide
component goes into solution only to a negligible extent there because of
poor solubility. The recycled flow of liquid is 1.2 l/min. A partial
stream of gas exiting from scrubbing column 10 is analyzed with NO.sub.x
analyzer 5 for its residual content of nitrogen oxides.
Conditions:
Model gas: 480 ppm NO and 680 ppm NO.sub.x
(200 ppm NO.sub.2) at 2.3 Nm.sup.3 /h
Temperature in the reactor: 40.degree. C.
Total pressure: 1 bar
The concentrations in the withdrawn gas are:
Without addition of solution of H.sub.2 O.sub.2 in 6: 430 ppm NO and 630
ppm NO.sub.x (200 ppm NO.sub.2);
With addition of 0.08 ml/min. H.sub.2 O.sub.2, 50% solution in 6:
0 ppm NO and 30 ppm NO.sub.x (30 ppm NO.sub.2).
These final concentrations are achieved 10 minutes after the start of the
dosing in of H.sub.2 O.sub.2. The silica gel, which was previously white,
assumes a yellowish color during the course of this time.
Degree of denitration: 95.6%.
Example 2
The method of operation corresponds to that of Example 1 but with modified
concentration of NO.sub.x of the model gas (700 ppm NO and 1000 ppm
NO.sub.x (300 ppm NO.sub.2) and with a dosing rate of 0.12 ml/min.
solution of H.sub.2 O.sub.2) into falling film evaporator 6 as well as
with the use of 50% nitric acid as absorption solution in 10.
After the addition of 0.12 ml/min. H.sub.2 O.sub.2 (50% solution) in 6, the
concentrations in the withdrawn gas are: 0 ppm NO and 460 ppm NO.sub.x
(460 ppm NO.sub.2).
The blind (control) test with model gas free of NO.sub.x and without the
addition of H.sub.2 O.sub.2 resulted in a signal of 0 ppm NO and 380 ppm
NO.sub.x (380 ppm NO.sub.2) in the withdrawn gas as a consequence of the
vapor pressure of the 50% nitric acid.
Degree of denitration: 92% (HNO.sub.3 vapor pressure taken into
consideration).
Example 3
As in Example 1 but with a different concentration of NO.sub.x of the model
gas (210 ppm NO and 350 ppm NO.sub.x (140 ppm NO.sub.2)), a catalytic
amount of 30 g silica gel and with a temperature of 25.degree. C. and a
dosing rate of 0.02 ml/min. solution of H.sub.2 O.sub.2.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 180 ppm NO and 320
ppm NO.sub.x (140 ppm NO.sub.2);
With addition of 0.02 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
8 ppm NO and 28 ppm NO.sub.x (20 ppm NO.sub.2).
Degree of denitration: 92%.
Example 4
Like Example 1 but the apparatus additionally contains a falling film
evaporator which is identical in design to falling film evaporator 6 but
connected in front of it and into which 0.3 ml/min. water are dosed for
humidifying the model gas. The temperature in the reactor is 65.degree. C.
and the solution of H.sub.2 O.sub.2 is added at 0.12 ml/min.
The concentrations in the withdrawn gas are:
Without addition of solution of H.sub.2 O.sub.2 in 6: 420 pp NO and 640 ppm
NO.sub.x (220 ppm NO.sub.2);
With addition of 0.12 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
20 ppm NO and 60 ppm NO.sub.x (40 ppm NO.sub.2).
These final concentrations are achieved 30 min. after the start of the
dosing of H.sub.2 O.sub.2. Condensation drops form over the catalyst but
do not disturb the operation of the fluid bed.
25 Degree of denitration: 91.2%.
Example 5
Like Example 4 but SO.sub.2 gas is additionally supplied to the model gas
corresponding with the addition of NO from gas bottle 1. (Model gas: 400
ppm NO and 720 ppm NO.sub.x (320 ppm NO.sub.2) as well as 130 ppm SO.sub.2
at 1.15 Nm.sup.3 /h). The temperature in the reactor is 40.degree. C. and
the volume flow of the model gas is 1.15 Nm.sup.3 /h. The solution of
H.sub.2 O.sub.2 is fed into evaporator 6 at 0.08 ml/min.
The withdrawn gas contains:
Without addition of H.sub.2 O.sub.2 in 6: 220 ppm NO and 680 ppm NO.sub.x
(460 ppm NO.sub.2) and 75 ppm SO.sub.2 ;
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
2 ppm NO and 55 ppm NO.sub.x (53 ppm NO.sub.2 and .about.0 ppm SO.sub.2.
These final concentrations are achieved after a few minutes as regards
SO.sub.2 and after one hour as regards NO and NO.sub.2. The silica gel
changes its color from white to orange.
Degree of denitration: 92.4%.
Example 6
Like Example 1 but the gas (model gas: humidified, 480 ppm NO and 720 ppm
NO.sub.x (240 ppm NO.sub.2)) is humidified as in Example 4 with water and
30 g catalyst (silica gel 60) are added. The reactor is operated at
different temperatures (25.degree. C., 80.degree. C., 110.degree. C. and
130.degree. C.) which are adjusted with electric strip heaters.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 410 ppm NO and 600
ppm NO.sub.x (190 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
11 ppm NO and 62 ppm NO.sub.x (51 pm NO.sub.2) at 25.degree. C. reactor
temperature, and
40 ppm NO and 100 ppm NO.sub.x (60 ppm NO.sub.2) at 80.degree. C., and
70 ppm NO and 180 ppm NO.sub.x (110 ppm NO.sub.2) at 110.degree. C., and
100 ppm NO and 240 ppm NO.sub.x (140 ppm NO.sub.2) at 130.degree. C.
These final concentrations are achieved on the average 40 min. after the
start of the dosing of H.sub.2 O.sub.2.
Degree of denitration:
91.4% at 25.degree. C.
86.1% at 80.degree. C.
75.0% at 110.degree. C.
66.7% at 130.degree. C.
Example 7
a) Like Example 1; however, the described system is followed in succession
by a further falling film evaporator identical in design to 6 and with
automatic dosing device, by a further fluidized bed reactor identical in
design to 9 which likewise contains 60 g silica gel and by a further
filler column identical in design to 10 which is operated in
countercurrent.
These additional apparatus are used for a second treatment stage. Filler
column 10 of the first treatment stage is used here for the intermediate
absorption of HNO.sub.3 from the gas phase. The content of NO and of
NO.sub.x is again determined both after filler column 10 and also from the
gas withdrawn from the total system.
Conditions, in deviation from Example 1:
Catalyst 2.times.60 g silica gel 60
Model-gas current: 480 ppm NO and 750 ppm NO.sub.x
(270 ppm NO.sub.2) at 1.5 Nm.sup.3 /h.
The withdrawn gas has:
Without addition of H.sub.2 O.sub.2 into one of the two evaporators, a
content of:
.about.420 ppm NO and 710 ppm NO.sub.x (290 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 into
evaporator 6 (1st stage), a content of:
12 ppm NO and 68 ppm NO.sub.x (56 ppm NO.sub.2);
With the additional addition of 0.02 ml/min. 50% solution of H.sub.2
O.sub.2 into the evaporator of the 2nd stage following the 1st treatment
stage:
1 ppm NO and 18 ppm NO.sub.x (17 ppm NO.sub.2).
Degree of denitration:
90.0% (stage 1)
73.5% (stage 2)
97.6% (total).
b) Like Example 7a; however, the apparatus is additionally provided with a
filler column operated with water of 25.degree. C. The latter is located
directly upstream of evaporator 6 and serves to humidify the model gas.
Moreover, there is no intermediate absorption of HNO.sub.3 after the 1st
stage. Rather, the gas stream is conducted from the 1st reactor directly
into the falling film evaporator of the 2nd stage, into which, however, no
solution of H.sub.2 O.sub.2 is dosed.
The withdrawn gas contains, upon the addition of 0.1 ml/min. 50% solution
of H.sub.2 O.sub.2 :
.about.0 ppm NO and 15 ppm NO.sub.x (15 ppm NO.sub.2).
Degree of denitration: 98% (total).
Example 8
Like Example 1 but with another catalyst and gas current reduced to 0.54
Nm.sup.3 /h. Instead of compressed air, room air is sucked through the
apparatus with the gas pump belonging to the NO.sub.x analyzer
Conditions, in deviation from Example 1:
Catalyst 10 g silica gel 60 H silanized (item 7761 of the Merck company,
Darmstadt)
Model gas: 300 ppm NO and 520 ppm NO.sub.x (220 ppm NO.sub.2) at 0.54
Nm.sup.3 /h external air as carrier gas.
The concentrations in the withdrawn gas are:
Without addition of solution of H.sub.2 O.sub.2 in 6: 270 ppm NO and 490
ppm NO.sub.x (220 ppm NO.sub.2);
With addition of 0.024 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
.about.0 ppm NO and 30 ppm NO.sub.x (30 ppm NO.sub.2).
Degree of denitration: 94.2%
Example 9
Like Example 1 but with another catalyst and at a temperature of 65.degree.
C. in the reactor.
Other conditions, in deviation from Example 1:
Catalyst: 10 g H mordenite (pore diameter 6.7.times.7.0 .ANG., modulus 18
(Si/Al =9) in granulated form, particle size 0.3-0.9 mm
Model gas: 550 ppm NO and 790 ppm NO.sub.x (240 ppm NO.sub.2) at 2.3
Nm.sup.3 /h.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 440 ppm NO and 720
ppm NO.sub.x (280 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 H.sub.2 in 6:
40 ppm NO and 210 ppm NO.sub.x (170 ppm NO.sub.2).
Degree of denitration: 73.4%.
Example 10
Like Example 1 but with reduced flow of model gas and another catalyst.
Conditions, in deviation from Example 1:
Catalyst Zeolite ZSM-5 (pore diameter 5.4-5.6 .ANG., modulus 42 (Si/Al =21)
in granulated form, particle size 0.3-0.9 mm
Model gas: 490 ppm NO and 700 ppm NO.sub.x (210 ppm NO.sub.2) at 1.58
Nm.sup.3 /h.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 370 ppm NO and 590
ppm NO.sub.x (220 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
.about.0 ppm NO and 120 ppm NO.sub.x (120 ppm NO.sub.2).
Degree of denitration: 82.9%.
b) Like Example 10 a but with another catalyst.
Conditions, in deviation from Example 10 a:
Catalyst: 20 g ion-exchange resin, macroporous, sharply acidic (Amberlyst
15, item 15 635 of the Merck company, Darmstadt), particle size 0.3-0.9
mm.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 390 ppm NO and 540
ppm NO.sub.x (150 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
40 ppm NO and 150 ppm NO.sub.x (110 ppm NO.sub.2).
Degree of denitration: 76.6%.
Example 11
a) Like Example 8 but with another catalyst.
Conditions, in deviation from Example 8:
Catalyst: 10 g H talcum powder, commercial product
Model gas: 350 ppm NO and 580 ppm NO.sub.x (230 ppm NO.sub.2).
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 310 ppm NO and 530
ppm NO.sub.x (230 ppm NO.sub.2);
With addition of 0.024 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
20 ppm NO and 210 ppm NO.sub.x (190 ppm NO.sub.2).
Degree of denitration: 63.8%.
b) Like Example 11 a but with another catalyst.
Conditions, in deviation from example 11 a:
Catalyst: 10 g diatomaceous earth, commercial product (item 8117 of the
Merck company, Darmstadt).
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 290 ppm NO and 530
ppm NO.sub.x (140 ppm NO.sub.2);
With addition of 0.024 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
10 ppm NO and 200 ppm NO.sub.x (190 ppm NO.sub.2).
Degree of denitration: 65.5%.
c) Like Example 11a but with another catalyst.
Conditions, in deviation from Example 11a:
Catalyst: 30 g Aluminum oxide powder (aluminum oxide 90, item 1078 of the
Merck company, Darmstadt).
The withdrawn gas contains, with the addition of 0.024 ml/min. 50% solution
of H.sub.2 O.sub.2 in 6:
.about.0 ppm NO and 43 ppm NO.sub.x (43 ppm NO.sub.2).
Degree of denitration: 92.6%.
d) Like Example 11a but with another catalyst.
Conditions, in deviation from Example 11a:
Catalyst: 30 g H titanium dioxide powder (item 812 of the Merck company,
Darmstadt).
The withdrawn gas contains, with the addition of 0.024 ml/min. 50% solution
of H.sub.2 O.sub.2 in 6:
.about.0 ppm NO and 55 ppm NO.sub.x (55 ppm NO.sub.2).
Degree of denitration: 90.5%.
Example 12
Like Example 1 but with another catalyst and reduced current of model gas.
Conditions, in deviation from Example 1:
Catalyst: 55 g material containing laminated silicate (Catsan hygienic
litter, Effem company, Verden), granulated, particle size <1 mm
Model gas: 500 ppm NO and 700 ppm NO.sub.x (200 ppm NO.sub.2) at 1.58
Nm.sup.3 /h.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 490 ppm NO and 550
ppm NO.sub.x (60 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
2 ppm NO and 45 ppm NO.sub.x (43 ppm NO.sub.2).
The final values with the addition of H.sub.2 O.sub.2 are achieved after 60
minutes.
Degree of denitration: 93.6%.
Example 13
Like Example 1, however, instead of fluidized bed reactor 9, a tube reactor
(material: glass, diameter 3 cm) with catalytic fixed bed is used. A
temperature of 65.degree. C. prevails in the reactor and the model gas
current is 2.0 Nm.sup.3 /h.
Other conditions, in deviation from Example 1:
Catalyst: 7.5 g activated carbon, extruded pieces 2.4.times.4 mm (specific
surface 1270 m.sup.2 /g) (activated-carbon carrier 120, Degussa company,
Frankfurt)
Model gas stream: 480 ppm NO and 720 ppm NO.sub.x (240 ppm NO.sub.2) at 2.0
Nm.sup.3 /h.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 440 ppm NO and 640
ppm NO.sub.x (200 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6: 40 ppm
NO and 410 ppm NO.sub.x (370 ppm NO.sub.2).
Degree of denitration: 43.1%.
Example 14
a) Like Example 13 but with another catalyst.
Conditions, in deviation from Example 13:
Catalyst: 30 g Zeolite H-mordenite, extruded pieces 4.times.7 mm, (pore
diameter 6.7.times.7.0 .ANG., modulus 18 (Si/Al=9)
Temperature: 65.degree. C.
Model gas stream: 510 ppm NO and 750 ppm NO.sub.x (240 ppm NO.sub.2) at 2.0
Nm.sup.3 /h.
The withdrawn gas contains:
Without addition of solution of H.sub.2 O.sub.2 in 6: 410 ppm NO and 650
ppm NO.sub.x (240 ppm NO.sub.2);
With addition of 0.08 ml/min. 50% solution of H.sub.2 O.sub.2 in 6:
20 ppm NO and 200 ppm NO.sub.x (180 ppm NO.sub.2).
Degree of denitration: 73.3%.
b) Like Example 13 but with elevated temperature.
Conditions, in deviation from Example 13:
Temperature: 100.degree. C.
The withdrawn gas contains, with the addition of 0.08 ml/min. 50% solution
of H.sub.2 O.sub.2 in 6:
0 ppm NO and 210 ppm NO.sub.x (210 ppm NO.sub.2).
Degree of denitration: 72%.
Further variations and modifications of the foregoing will be apparent to
those skilled in the art and are intended to be encompassed by the claims
appended hereto.
German application P 40 15 284.7-43 is relied on and incorporated herein.
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